TW202227766A - 以混合氣體渦輪機低溫分離空氣之方法及裝置 - Google Patents

以混合氣體渦輪機低溫分離空氣之方法及裝置 Download PDF

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TW202227766A
TW202227766A TW110134752A TW110134752A TW202227766A TW 202227766 A TW202227766 A TW 202227766A TW 110134752 A TW110134752 A TW 110134752A TW 110134752 A TW110134752 A TW 110134752A TW 202227766 A TW202227766 A TW 202227766A
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column
argon
gas
pressure column
condenser
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TW110134752A
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English (en)
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迪米特里 高盧貝夫
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德商林德有限公司
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
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    • F25J3/04096—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of argon or argon enriched stream
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
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    • F25J3/04321—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of oxygen
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

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Abstract

在此用於低溫分離空氣的方法及裝置中，分離管柱系統包含高壓管柱(12)、低壓管柱(13)、及粗氬管柱(18)。藉由將氣態氧(72)與來自氬頂部冷凝器(21)之蒸發空間的氣體流(31、71)混合所生成的混合氣體流(73、74)係在混合氣體渦輪機(75)中功膨脹。

Description

以混合氣體渦輪機低溫分離空氣之方法及裝置
本發明係關於根據獨立專利請求項之第一部分之用於低溫分離空氣之方法及各別裝置。
產生氣態及液體產物之空氣的低溫分離大致上已從例如H.-W. Häring, Industrial Gases Processing, Wiley-VCH, 2006，尤其第2.2.5節，「低溫精餾(Cryogenic Rectification)」所得知。
低溫空氣分離單元典型包含呈雙管柱系統形式(尤其是Linde雙管柱)的分離管柱系統。其等亦可具有三管柱或更多管柱系統的形式。除了那些用於產生呈液體及/或氣態形式的氮及/或氧的氧-氮分離管柱以外，分離管柱系統可包含額外的管柱以用於收回另外的空氣組分(尤其是稀有氣體)或者用於生成特定的高純度氧及/或氮產物。
在本發明中，使用高壓管柱及低壓管柱，低壓管柱可至少部分地位於高壓管柱及主冷凝器上方。本發明之方法係增強壓力的類型，使得高壓管柱並未在約5.3巴(4至7巴)的典型壓力下而是在例如8至14巴(較佳地9至13巴)的較高壓力下進行操作。低壓管柱並未在約1.3巴(1.2至1.5巴)的典型壓力下而是在例如2至5巴(較佳地2.5至4.5巴)的較高壓力下進行操作。那些壓力係絕對的，且欲在各別管柱的頂部處測量且亦用在本發明中。
若空氣分離器生成加壓氣態產物，則其等可在氣體壓縮機(「外部壓縮」)中壓縮。或者，「內部壓縮」方法可藉由從管柱抽出低溫液體、將其加壓(例如抽泵)至所欲壓力、及藉由例如在主熱交換器中加溫而將其轉換成氣態狀態來使用。
本發明所具有的目標在於找出進一步改善的空氣分離方法，尤其針對加壓氮及氬的共同生成以及相對高的液體產量(例如，液體產量(LIN等效[Nm3/h]: LIN [Nm3/h] + 1.07 × LOX [Nm3/h] + 0.9 × LAR [Nm3/h])除以加壓GAN產物量處於從0.00至0.06的範圍內)。(在本申請案中，只要未作相反陳述，所有那些量均係莫耳的。)
此類目標係藉由根據獨立專利請求項之方法及裝置來解決。
從高壓管柱抽出並引入低壓管柱中的餾分常係高壓管柱的底部餾分。其之至少一部分最終可通過低溫冷卻器直接引入低壓管柱中，或者可藉由將高壓管柱餾分導入氬頂部冷凝器蒸發空間中並分別從氬頂部冷凝器蒸發空間將氣體及剩餘液體引入低壓管柱而間接地完成。
氣態氧流正常情況下係從低壓管柱的下部部分(例如，從低壓管柱的極底部)抽出。
膨脹機器可係任何類型(例如渦輪機)；則可將其稱為「混合氣體渦輪機」。
為了增強低壓管柱內的精餾，可如技術方案2中所述般使用來自低壓管柱且直接或間接地導入分離管柱系統，尤其高壓管柱及/或低壓管柱中的氮回收。「回收氣體」流係來自低壓管柱、在氮壓縮機中經壓縮、然後在主熱交換器中經冷卻但未液化者。來自低壓管柱的產物氣體可或可不與回收氣體共同經引導通過主熱交換器中的加溫及氮壓縮機中的壓縮。經冷卻的回收氣體可例如在頂部或理論上下方3至11個托盤處至少部分地直接以氣態形式經引導至高壓管柱中。一替代方案係例如藉由在冷凝器(例如主冷凝器)及/或另一管柱再沸器中將回收氣體液化並接著將經液化的回收氣體之至少一部分引入管柱，尤其高壓管柱及/或低壓管柱中來間接地引入高壓管柱及/或低壓管柱中。在第一實例中，經冷卻之回收氣體的至少一部分係經由主冷凝器的液化空間引入高壓管柱中。在另一實例中，經冷卻的回收氣體的至少一部分通過純氧管柱之底部冷凝器的液化空間引入至低壓管柱中(較佳地包括在低溫冷卻器中在單獨通道中低溫冷卻此液體且將該經低溫冷卻的液體在膨脹閥中膨脹)。舉例而言，回收氣體的第一部分經第一路徑(例如直接或經主冷凝器)導入至高壓管柱且回收氣體的第二部分經第二路徑(例如通過純氧管柱的底部冷凝器)導入至低壓管柱。
在第一變化例中，經冷卻的回收氣體可例如在頂部處直接引入高壓管柱中。技術方案3描述第二變化例，其中回收氣體係引入主冷凝器中，在其中經液化，並接著作為液體引入至高壓管柱的頂部上。兩變化例可藉由將冷的回收氣體之一部分引入主冷凝器中，再將另一部分直接地引入管柱中而組合。回收氣體的另一部分可用在廠內的不同處。
加壓純氬產物可藉由內部壓縮而產生，如技術方案4中所指示者。總氬產物的一部分可以液體形式生成並儲存在儲槽中。
粗氬管柱可具有如技術方案5所述之分離管柱的形式。有至少兩個部分。原則上，可有三或更多個部分。
分離可進一步包含如技術方案6所述之純氧管柱。用於純氧管柱之進給液體來自粗氬管柱之底部或來自粗氬管柱之中間點(例如，理論上底部上方的數個托盤處)。
此類純氧管柱較佳地係配置在粗氬管柱的第一部分下方並與粗氬管柱之第一部分配置在共用容器內之純氧管柱。
純氧管柱較佳地具有如技術方案8所述的底部再沸器，其可加熱高壓管柱氣態氮及/或不直接進入高壓管柱中之一部分的經冷卻回收氣體-請參見技術方案9。回收氣體較佳地至少部分地在純氧管柱的底部再沸器中經液化，並接著作為回流液體送至高壓管柱或至低壓管柱。
在不需要整個氬產物的操作模式中，可根據技術方案10經由中間氣體出口從粗氬管柱抽出氬-氧混合物。該特徵減少粗氬管柱之負載。為了收回其能量，在主熱交換器中加溫氬-氧混合物。
此特定實施例適用於單件式粗氬管柱及分離式粗氬管柱。在最後一種情況下，中間氣體出口可在粗氬管柱的任一部分中。較佳地，其係配置在第二部分的中間高度處。
在本發明中，可係有利的是使用如技術方案11所述之分離式低壓管柱。
在一方法變化例中，較佳地沒有回收氣體，且高壓管柱(12)的頂部氣體係抽出(302)作為加壓氣態氮產物，如技術方案13所指示者。替代或額外地，來自低壓管柱(13、113/213)的頂部氣體(64、65)係在氮壓縮機中經壓縮，並抽出作為加壓氣態氮產物，尤其係藉由將其與來自高壓管柱(12)的經加溫頂部氣體混拌。氮壓縮機較佳地未壓縮更多流，尤其無回收氣體。
在 圖 1的實施例中，大氣空氣(AIR)1流過過濾器2至主空氣壓縮機3，並在其中經壓縮至約11至12巴的壓力。經壓縮的空氣流係在冷卻器4及5中冷卻，並送至從其中排出液體水(H2O)之分離器6。來自分離器6的空氣係送至純化單元7，藉由吸附移除水蒸氣、二氧化碳、及附加的雜質。經純化的空氣8係引入主熱交換器9中。總進給空氣係經完全冷卻直到主熱交換器9的冷端，並接著引入進一步包含低壓管柱13及主冷凝器14之雙管柱的高壓管柱12。
圖1之實施例之分離管柱系統由雙管柱12/13、純氧管柱16、甲烷排除管柱17、單件式粗氬管柱18、及純氬管柱19組成。純氧管柱具有底部再沸器20，粗氬管柱具有頂部冷凝器21，且純氬管柱具有頂部冷凝器22及底部再沸器23。所有這些冷凝器及再沸器以及主冷凝器14係冷凝器-蒸發器，其等各具有液化空間及蒸發空間。純氬管柱19的底部再沸器23係一例外，其係藉由顯熱來加溫。
來自高壓管柱12之底部的粗液氧24係在低溫冷卻器25中冷卻。經冷卻的粗液氧26之第一部分27係部分地饋送通過純氬管柱的底部再沸器23，並接著引入粗氬管柱18之頂部冷凝器21的蒸發空間中。剩餘液體28係送至低壓管柱13。經蒸發部分29的第一部分30亦送至低壓管柱。根據本發明將第二部分31取為「具有較高氮含量的流」31，且其將在稍後詳述。
經冷卻粗液氧26的第二部分32係引入純氬管柱19之頂部冷凝器的蒸發空間中。剩餘液體33係送至低壓管柱13。經蒸發部分34係混合至來自粗氬管柱18之頂部冷凝器21的蒸發空間之經蒸發部分29。由此前往低壓管柱13或進入「具有較高氮含量的流」31。
來自高壓管柱12頂部之氣態氮35的大多數36係至少部分地在主冷凝器14中液化。剩餘部分37係在純氧管柱的底部再沸器中至少部分地液化。來自純氧管柱底部再沸器的液氮係在低溫冷卻器25中冷卻。經冷卻的液氮39係送至低壓管柱13的頂部。
來自主冷凝器14的液氮40係部分地饋回至高壓管柱12的頂部。另一部分42係在低溫冷卻器25中冷卻。經冷卻的液氮43之第一部分係送至低壓管柱13的頂部，而第二部分45則係抽出作為純液氮產物(PLIN)。
來自低壓管柱13之氣態含氬餾分(氬過渡餾分46)係引入甲烷排除管柱17的底部中。在另一方向上，甲烷排除管柱17之底部液體47係再引入低壓管柱13中。此類底部液體實際上含有所有來自餾分46的甲烷，使得甲烷排除管柱17的頂部係無甲烷的。此類管柱之頂部氣體48係連同來自純氧管柱16的頂部氣體80一起送至粗氬管柱18的底部。
粗氬管柱18的底部液體78係經由泵79舉升。第一部分49作為無甲烷回流進入純氧管柱16。從純氧管柱16的底部抽出超高純度液氧50，並將其導入儲存槽51中。儲槽液體可藉由泵(未圖示)而在儲槽中或在儲槽下游加壓。高壓液氧可在主熱交換器9中加溫，並收回作為經內部壓縮之超高純度氣態氧產物(GOXIC)。
粗氬管柱18之底部液體78的第二部分52係饋入甲烷排除管柱17之頂部中。
粗氬管柱18之頂部冷凝器21的液化空間係浴型冷凝器。在其頂部處，粗氬流58係從粗氬管柱18抽出並引入純氬管柱19中。從純氬管柱的頂部，抽出廢氣60並將其釋放至大氣(ATM)。在底部處，收回純氬產物59，並以泵61及(線62)將其送至內部壓縮，在主熱交換器9中加溫。在主熱交換器9的加溫端(線63)，經內部壓縮的氣態氬產物(GARIC)係以加壓形式抽出。
來自低壓管柱13頂部的氣態氮餾分64係部分地用作回收氣體，且首先在低溫冷卻器25中預加溫。經預加溫的氣態氮餾分65係送至主熱交換器9的冷端並在其中經完全加溫。經加溫的氣態氮餾分66係在氮壓縮機67中壓縮至較佳地8至15巴、更佳地9,5至12,5巴的產物壓力。壓縮機67具有後冷卻器。經壓縮的氮餾分68係分成產物餾分69及回收氣體70，該產物餾分係作為經加壓氣態氮產物(PGAN)抽出。經加壓回收氣體係在主熱交換器9中再次完全冷卻。經冷卻的回收氣體(89)係與來自高壓管柱12頂部的氣態氮35混合，亦即，在主冷凝器14或純氧管柱底部再沸器20中經液化。由此，回收氣體的一部分(現作為液體)經由線41進入高壓管柱。
加壓氣態氧係藉由內部壓縮生成。來自低壓管柱13底部(或來自主冷凝器14之蒸發空間)的液氧84在泵85中泵抽至所欲的產物壓力，在主熱交換器9中完全加溫，且最終作為經內部壓縮產物(GOXIC)經由線86收回。
先前提及之至少部分地來自粗氬管柱18之頂部冷凝器21的蒸發空間之「具有較高氮含量的流」31係在低溫冷卻器25中加溫。經加溫的流71係與來自低壓管柱13底部的氣態氧流72混合。混合氣體73係在主熱交換器9中部分地加溫至150至230 K的中間溫度，並在操作為產生器渦輪機的混合氣體渦輪機75中功膨脹。經膨脹的混合氣體76係再引入主熱交換器9中並經完全加溫。經加溫的低壓混合氣體77/78可釋放至大氣(ATM)或送至純化單元7作為再生氣體。
在圖1之實施例中，可經由中間氣體出口81抽出在粗氬管柱18中上升的氣體之一些者，以便減少氬產物59/62/63的量，並從而降低能量消耗。氣體抽出氣體82係在主熱交換器9之分開通道中經完全加溫。經加溫的氣體83可混拌至經膨脹的混合氣體77，並釋放至大氣或用作純化單元7中的再生氣體。
圖 2之方法與圖1的主要不同之處在於分離式氬管柱及分離式低壓管柱。上文之圖1的解釋亦有效於圖2之各別步驟及單元。圖2中的參考編號部分係取自圖1，以便識別相同或類似的特徵及功能。
粗氬管柱係分成第一部分118及第二部分218，氬頂部冷凝器21經配置在第二部分218之頂部上。來自第一部分118頂部的氣體餾分190係引入第二部分218之底部。第二部分218之底部液體191的至少第一部分193係引入第一部分118之頂部中。
低壓管柱係分成底部部分113及頂部部分213。不同於單件式低壓管柱，那兩個部分係並排地配置。氣態連接流195係取自底部區段的頂部氣體194，並引入頂部區段213的底部中。液體連接流196係從頂部區段213的底部抽出，並經由粗氬管柱之第一部分118的底部、線197、泵198、及線199送至底部區段213的頂部。低壓管柱之底部區段113之頂部氣體194的另一部分係取為氬過渡餾分46，並引入粗氬管柱之第一部分118的底部中。第一部分118的底部液體(與來自低壓管柱之頂部部分213的底部液體196混合)係經由線197、泵198、及線199送至低壓管柱之底部部分113的頂部。
粗氬管柱之第一部分118的最下部區段117同時充當甲烷排除管柱。在緊接位於最下部區段117上方的中間高度處，第一部分118係藉由液體線149及氣體線180連接至純氧管柱16的頂部。
來自純氧管柱16之底部的超高純度液氧50在此特定實施例中係根據US 10209004 B2於多儲槽系統200中加壓，並接著(經由線201)在主熱交換器9中完全加溫。溫熱的超高純度氧氣202係收回作為最終產物(UHPGOX)。
來自低壓管柱113底部(或來自主冷凝器14之蒸發空間)的液氧84在低溫冷卻器25(未圖示)中經低溫冷卻，並接著抽出作為液氧產物(LOX)。
經冷卻的回收氣體89係(與來自高壓管柱12之頂部氮35的一些一起)饋送至主冷凝器14之液化空間。其在此處液化。經液化之回收氣體的第一部分41係饋送至高壓管柱12的頂部；經液化之回收氣體的第二部分42、44係饋送至低壓管柱213之頂部。
或者，經冷卻的回收氣體89可分成至主冷凝器之第一部分及引入至純氧管柱16之底部再沸器的液化空間的第二部分。在另一替代方案中，回收氣體完全饋送至純氧管柱16之底部再沸器的液化空間，該液化空間必要時用來自高壓管柱12之頂部的一些氣態氮35補充。
圖 3在許多部分均與圖2類似或完全相同，但在兩主要方面有所偏離： -      氣態氮係來自高壓管柱頂部，並經由線300、301、及302抽出作為加壓氣態氮產物(UHPGAN)。 -      沒有回收氣體。來自低壓管柱213之頂部氣態氮64/65/66/369的全部者係藉由將其混拌至來自高壓管柱12的氮而在氮壓縮機67下游抽出作為加壓氣態氮產物(UHPGAN)。
本發明大致上亦可應用至無甲烷排除管柱及/或無純氧管柱的系統。
1:大氣空氣(AIR) 2:過濾器 3:主空氣壓縮機 4:冷卻器 5:冷卻器 6:分離器 7:純化單元 8:經純化的空氣 9:主熱交換器 10:引入 12:高壓管柱 13:低壓管柱 14:主冷凝器 16:純氧管柱 17:甲烷排除管柱 18:單件式粗氬管柱 19:純氬管柱 20:底部再沸器 21:頂部冷凝器 22:頂部冷凝器 23:底部再沸器 24:粗液氧；餾分 25:低溫冷卻器 26:經冷卻的粗液氧；餾分 27:經冷卻的粗液氧之第一部分；液體冷卻餾分 28:剩餘液體 29:經蒸發部分 30:經蒸發部分之第一部分 31:第二部分；具有較高氮含量的流 32:經冷卻粗液氧之第二部分 33:剩餘液體 34:經蒸發部分 35:氣態氮 36:氣態氮的大多數 37:剩餘部分 39:經冷卻的液氮 40:液氮 41:線 42:另一部分 43:經冷卻的液氮 45:經冷卻的液氮之第二部分 46:餾分 47:甲烷排除管柱之底部液體 48:頂部氣體 49:第一部分 50:超高純度液氧 51:儲存槽 52:粗氬管柱之底部液體的第二部分 58:粗氬流 59:純氬產物 60:廢氣 61:泵 62:線 63:線 64:頂部氣體 65:頂部氣體 66:經加溫的氣態氮餾分 67:氮壓縮機 68:經壓縮的氮餾分 69:產物餾分 70:回收氣體 71:經加溫的流 72:氣態氧流 73:混合氣體 74:經加溫的混合氣體流 75:膨脹機器；混合氣體渦輪機 76:經膨脹的混合氣體流 77:經加溫的低壓混合氣體 78:底部液體；經加溫的低壓混合氣體 79:泵 80:頂部氣體 81:中間氣體出口；氬-氧混合物 82:氣體抽出氣體 83:經加溫的氣體 84:液氧 85:泵 86:線 89:經冷卻的回收氣體 113:低壓管柱；底部部分；底部區段 117:最下部區段 118:粗氬管柱之第一部分 149:液體線；液體餾分 180:氣體線 190:氣體餾分 191:底部液體 193:第一部分 194:氣態連接流；頂部氣體 195:氣態連接流 196:液體連接流；底部液體 197:液體連接流；線 198:泵 199:液體連接流；線 200:多儲槽系統 201:線 202:溫熱的超高純度氧氣 213:低壓管柱；頂部部分；頂部區段 218:粗氬管柱之第二部分 300:高壓管柱之頂部氣體的一部分；線 301:經加溫氣體；線 302:抽出；線 369:經壓縮氣體
本發明及本發明之進一步的細節將在下文中藉由例示性實施例來說明，該等例示性實施例係顯示於圖式中。
圖1具有單件式低壓管柱之本發明的第一實施例， 圖2具有分離式低壓管柱之第二實施例及 圖3第三實施例，其中從高壓管柱頂部部分地抽出GAN產物
1:大氣空氣(AIR)
2:過濾器
3:主空氣壓縮機
4:冷卻器
5:冷卻器
6:分離器
7:純化單元
8:經純化的空氣
9:主熱交換器
10:引入
12:高壓管柱
13:低壓管柱
14:主冷凝器
16:純氧管柱
17:甲烷排除管柱
18:單件式粗氬管柱
19:純氬管柱
20:底部再沸器
21:頂部冷凝器
22:頂部冷凝器
23:底部再沸器
24:粗液氧；餾分
25:低溫冷卻器
26:經冷卻的粗液氧；餾分
27:經冷卻的粗液氧之第一部分；液體冷卻餾分
28:剩餘液體
29:經蒸發部分
30:經蒸發部分之第一部分
31:第二部分；具有較高氮含量的流
32:經冷卻粗液氧之第二部分
33:剩餘液體
34:經蒸發部分
35:氣態氮
36:氣態氮的大多數
37:剩餘部分
39:經冷卻的液氮
40:液氮
41:線
42:另一部分
43:經冷卻的液氮
45:經冷卻的液氮之第二部分
46:餾分
47:甲烷排除管柱之底部液體
48:頂部氣體
49:第一部分
50:超高純度液氧
51:儲存槽
52:粗氬管柱之底部液體的第二部分
58:粗氬流
59:純氬產物
60:廢氣
61:泵
62:線
63:線
64:頂部氣體
65:頂部氣體
66:經加溫的氣態氮餾分
67:氮壓縮機
68:經壓縮的氮餾分
69:產物餾分
70:回收氣體
71:經加溫的流
72:氣態氧流
73:混合氣體
74:經加溫的混合氣體流
75:膨脹機器；混合氣體渦輪機
76:經膨脹的混合氣體流
77:經加溫的低壓混合氣體
78:底部液體；經加溫的低壓混合氣體
79:泵
80:頂部氣體
81:中間氣體出口；氬-氧混合物
82:氣體抽出氣體
83:經加溫的氣體
84:液氧
85:泵
86:線
89:經冷卻的回收氣體

Claims (15)

  1. 一種用於在分離管柱系統中低溫分離空氣之方法，該分離管柱系統包含：高壓管柱(12)；低壓管柱(13)；主冷凝器(14)，其係具有液化空間及蒸發空間的冷凝器-蒸發器，並使高壓管柱頂部與低壓管柱底部處於熱交換關係；及粗氬管柱(18)，其具有氬頂部冷凝器(21)，該氬頂部冷凝器係具有液化空間及蒸發空間的冷凝器-蒸發器，該方法包含 壓縮(3)總進給空氣流(1)， 在主熱交換器(9)中冷卻該經壓縮進給空氣(8)， 將該進給空氣的至少一部分引入(10)該高壓管柱(12)中， 從該高壓管柱(12)直接或間接地引入至少一餾分(24、26)至該低壓管柱(13)， 從該低壓管柱(13)引入氬過渡餾分(46、48)至該粗氬管柱(18)， 將液體冷卻餾分(27)從該高壓管柱(12)引入該氬頂部冷凝器(21)之該蒸發空間中， 從該低壓管柱(13)抽出氣態氧流(72)， 將該氣態氧流(72)與具有高於該氣態氧流之氮含量的另一氣體流混合，以形成混合氣體流(73)， 在該主熱交換器(9)中加溫該混合氣體流， 在膨脹機器(75)中使該經加溫的混合氣體流(74)功膨脹，且 在該主熱交換器(9)中完全加溫該經膨脹的混合氣體流(76)， 其特徵在於具有較高氮含量的該上述流(29、31、71)係從該氬頂部冷凝器(21)的該蒸發空間抽出。
  2. 如請求項1之方法，其中 來自該低壓管柱(13)的氣態氮餾分(64、65)係用作回收氣體， 該回收氣體係在該主熱交換器(9)中經加溫， 該經加溫的回收氣體(66)係在氮壓縮機(67)中壓縮； 該經壓縮的回收氣體(70)係在該主熱交換器(9)中冷卻，且以氣態形式自該主熱交換器(9)抽出；且 該經冷卻的回收氣體(89)之至少第一部分係以氣態形式或液化形式引入該分離管柱系統，尤其該高壓管柱(12)及/或該低壓管柱(13)中。
  3. 如請求項2之方法，其中該經冷卻回收氣體(89)之至少一部分係經由該主冷凝器(14)之該液化空間引入(36、40、41)該高壓管柱(12)中。
  4. 如請求項1至3之方法，其中 該分離管柱系統進一步包含純氬管柱(19)， 粗氬流(58)係從該粗氬管柱(18)或該氬頂部冷凝器(21)抽出， 該粗氬流(58)係引入該純氬管柱(19)中， 液體純氬流(59)係從該純氬管柱(19)抽出， 該液體純氬流(59)係在液體狀態下加壓(61)， 該經加壓的純氬流(62)係在該主熱交換器(9)中加溫，且 最終經收回作為經加壓氬產物(63)。
  5. 如請求項1至4之方法，其中該粗氬管柱係分成第一部分(118)及第二部分(218)，該氬頂部冷凝器(21)係配置在該第二部分(218)之頂部上，藉此來自該第一部分(118)之頂部的氣體餾分(190)係引入該第二部分(218)之底部，且該第二部分之該底部液體(191)的至少第一部分(193)係引入該第一部分(118)的該頂部中。
  6. 如請求項5之方法，其中 該分離管柱系統進一步包含純氧管柱(16)， 來自該粗氬管柱(18、118)之液體餾分(49、149)係引入該純氧管柱(16)的頂部中，且 液體純氧餾分(50)係從該純氧管柱(16)的底部抽出。
  7. 如請求項6之方法，其中該純氧管柱(16)係配置為緊接在甲烷排除管柱(17)下方，在彼此之間僅具有單一底板/頂板 。
  8. 如請求項6或7之方法，其中該純氧管柱(16)具有底部再沸器(20)，其係具有液化空間及蒸發空間的冷凝器-蒸發器。
  9. 如請求項2及8之方法，其中該經冷卻回收氣體(89)之第二部分(37)係引入該純氧管柱底部再沸器(20)的該液化空間中。
  10. 如請求項1至9之方法，其中至少暫時地，氬-氧混合物(81)係經由中間氣體出口從該粗氬管柱(18、118)抽出，且該氬-氧混合物係在該主熱交換器(9)中加溫。
  11. 如請求項1至10之方法，其中 該低壓管柱係分成底部部分(113)及頂部部分(213)， 氣態連接流(194、195)係從該底部區段(113)的頂部抽出， 該氣態連接流(195)係引入該頂部區段(213)的底部中， 液體連接流(196、197、199)係從該頂部區段(213)的該底部抽出，且 該液體連接流係引入該底部區段(113)之該頂部中。
  12. 如請求項1或4至11之方法，其中 該高壓管柱(12)之該頂部氣體的一部分(300)係在該主熱交換器(9)中加溫；且 該經加溫氣體(301)係抽出(302)作為加壓氣態氮產物。
  13. 如請求項1或4至12之方法，其中 來自該低壓管柱(13、113/213)的頂部氣體(64、65)係在該主熱交換器(9)中經加溫； 該經加溫氣體(66)係在氮壓縮機(67)中壓縮；且 該經壓縮氣體(369)係抽出(302)作為加壓氣態氮產物，尤其藉由將其混拌來自該高壓管柱(12)之該經加溫頂部氣體。
  14. 如請求項1至13之方法，其中該經冷卻回收氣體(89)係以氣態形式引入至該高壓管柱(12)中。
  15. 一種用於低溫分離空氣之裝置，其包含分離管柱系統，該分離管柱系統包含：高壓管柱(12)；低壓管柱(13)；主冷凝器(14)，其係具有液化空間及蒸發空間的冷凝器-蒸發器，並經組態使高壓管柱頂部與低壓管柱底部處於熱交換關係；及粗氬管柱(18)，其具有氬頂部冷凝器(21)，該氬頂部冷凝器係具有液化空間及蒸發空間的冷凝器-蒸發器，且該裝置進一步包含 主空氣壓縮機(3)，其用於壓縮總進給空氣流(1)， 主熱交換器(9)，其用於冷卻該經壓縮進給空氣(8)， 用於將該進給空氣的至少一部分引入該高壓管柱(12)中的構件(19)， 將來自該高壓管柱(12)的至少一餾分(24、26)直接或間接地引入該低壓管柱(13)的構件， 氬過渡線，其用於從該低壓管柱(13)引入氬過渡餾分(46、48)至該粗氬管柱(18)， 用於將液體冷卻餾分(27)從該高壓管柱(12)引入該氬頂部冷凝器(21)之該蒸發空間中的構件， 用於從該低壓管柱(13)抽出氣態氧流(72)的構件， 用於將該氣態氧流(72)與具有高於該氣態氧流之氮含量的另一氣體流混合以形成混合氣體流(73)的構件， 用於將該混合氣體流引入該主熱交換器(9)中以進行加溫的構件， 膨脹機器(75)，其用於使該經加溫混合氣體流(74)功膨脹，及 用於在該主熱交換器(9)中完全加溫該經膨脹的混合氣體流(76)的構件， 其特徵在於用於將該氣態氧流(72)與具有較高氮含量的另一氣體流混合的構件(29、31、71)係經連接至該氬頂部冷凝器(21)的該蒸發空間。
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CN116171366A (zh) 2023-05-26
WO2022058043A1 (en) 2022-03-24
KR20230069966A (ko) 2023-05-19

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